US4865540A - Air flow measurement device for fluidized bed reactor - Google Patents

Air flow measurement device for fluidized bed reactor Download PDF

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Publication number
US4865540A
US4865540A US07/304,998 US30499889A US4865540A US 4865540 A US4865540 A US 4865540A US 30499889 A US30499889 A US 30499889A US 4865540 A US4865540 A US 4865540A
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United States
Prior art keywords
air
fluidized bed
pressure sensing
bed reactor
sensing means
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Expired - Fee Related
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US07/304,998
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English (en)
Inventor
Francis D. Fitzgerald
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Foster Wheeler Energy Corp
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Foster Wheeler Energy Corp
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Priority to US07/304,998 priority Critical patent/US4865540A/en
Assigned to FOSTER WHEELER ENERGY CORPORATION, A CORP. OF DE reassignment FOSTER WHEELER ENERGY CORPORATION, A CORP. OF DE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: FITZGERALD, FRANCIS D.
Priority to CA000606485A priority patent/CA1311157C/en
Priority to JP1200428A priority patent/JPH0682055B2/ja
Application granted granted Critical
Publication of US4865540A publication Critical patent/US4865540A/en
Priority to CN89107388A priority patent/CN1021478C/zh
Priority to EP19900300943 priority patent/EP0381438A3/de
Priority to PT93042A priority patent/PT93042A/pt
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N1/00—Regulating fuel supply
    • F23N1/02—Regulating fuel supply conjointly with air supply
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/0007—Pressure measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00088—Flow rate measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N2225/00—Measuring
    • F23N2225/04—Measuring pressure
    • F23N2225/06—Measuring pressure for determining flow

Definitions

  • This invention relates to a fluidized bed reactor, and, more particularly, to such a reactor in which the rate of air flow to the fluidized bed of the reactor is measured.
  • Fluidized bed reactors including steam generators, combustors and gasifiers, are well known.
  • air is passed through a perforated plate, or the like, which supports a bed of particulate material, including a fossil fuel such as coal and an adsorbent for the sulfur generated as a result of combustion of the coal, to fluidize the bed and to promote the combustion of the fuel at a relatively low temperature.
  • a perforated plate or the like, which supports a bed of particulate material, including a fossil fuel such as coal and an adsorbent for the sulfur generated as a result of combustion of the coal, to fluidize the bed and to promote the combustion of the fuel at a relatively low temperature.
  • the heat produced by the fluidized bed is utilized to convert water to steam, such as in a steam generator, the fluidized bed system offers an attractive combination of high heat release, high sulfur adsorption, low nitrogen oxides emissions and fuel flexibility.
  • the most typical fluidized bed combustion system is commonly referred to as a bubbling fluidized bed in which a bed of particulate material is supported by an air distribution plate. Combustion-supporting air is introduced to the bed of particulate material through a plurality of perforations in the plate, causing the material to expand and take on a suspended or fluidized state.
  • the reactor is in the form of a steam generator
  • the walls of the reactor are formed by a plurality of heat transfer tubes.
  • the heat produced by combustion within the fluidized bed is transferred to a heat exchange medium, such as water, circulating through the tubes.
  • the heat transfer tubes are usually connected to a natural water circulation circuitry, including a steam drum, for separating water from the steam thus formed which is routed to a turbine to generate electricity or to a steam user.
  • a fluidized bed reactor has been developed utilizing a fast, or circulating, fluidized bed.
  • fluidized bed densities between 5% and 20% volume of solids are attained which is well below the 30% volume of solids typical of the bubbling fluidized bed.
  • the formation of the low density circulating fluidized bed is due to its small particle size and to a high solids throughput, which requires high solids recycle.
  • the velocity range of a circulating fluidized bed is between the solids terminal, or free fall, velocity and a velocity which is a function of the throughput, beyond which the bed would be converted into a pneumatic transport line.
  • the high solids circulation required by the circulating fluidized bed makes it insensitive to fuel heat release patterns, thus minimizing the variation of the temperature within the combustor or gasifier, and therefore decreasing the nitrogen oxides formation. Also, the high solids loading improves the efficiency of the mechanical device used to separate the gas from the solids for solids recycle. The resulting increase in sulfur adsorbent and fuel residence times reduces the adsorbent and fuel consumption. Furthermore, the circulating fluidized bed inherently has more turndown than the bubbling fluidized bed.
  • the bed of particulate material is supported by an air distribution plate.
  • An air plenum is located below the air distribution plate and the plenum receives air from a circulation device such as a fan.
  • the combustion supporting air is passed from the air plenum through openings or perforations in the air distribution plate to fluidize the particulate material. is important that the air flow to the bed of particulate material be measured to ensure that the flow of air to the bed is sufficient to maintain the fluidized state of the bed and, in the case of a circulating fluidized bed, to ensure the bed is not converted to a pneumatic transport line.
  • the conventional methods of measuring air flow to the bed of particulate material present many disadvantages and drawbacks.
  • a first conventional method requires placing an orifice plate or venturi in a long section of ducting between the fan and the plenum, negating the possibility of a compact reactor design
  • a second conventional method requires the utilization of a hot wire anemometer or a honeycomb device which greatly adds to the capital expense and operating costs of the reactor.
  • the fluidized bed reactor of the present invention includes an air distribution plate adapted to support a bed of particulate material including fuel.
  • a plurality of nozzles extend through the plate for receiving air from an air plenum and discharging the air in an upward direction into the bed at a velocity sufficient to fluidize the bed material and support the combustion or gasification of said fuel.
  • a pressure sensing unit is disposed within at least one of the nozzles and within the air plenum whereby the rate of air flow into the bed of particulate material can be determined from the difference in pressure between the nozzle and the air plenum.
  • Fig. 1 is a vertical sectional view depicting the fluidized bed reactor of the present invention
  • FIG. 2 is an enlarged partial sectional view of a portion of the air distribution plate and a nozzle utilized in the fluidized bed reactor of Fig. 1;
  • Fig. 3 is a view similar to Fig. 2, but depicting an alternate embodiment of a nozzle utilized in the fluidized bed reactor of Fig. 1;
  • Fig. 4 is also a view similar to Fig. 2, but depicting an alternate embodiment of a nozzle utilized in the fluidized bed reactor of Fig. 1.
  • the reference numeral 10 refers in general to an enclosure forming a major portion of a fluidized bed heat exchanger, or reactor, which may be in the form of a boiler, combustor, or any similar type device.
  • the enclosure 10 consists of a front wall 12, a rear wall 14, and two sidewalls, one of which is shown by the reference numeral 16.
  • the upper portion of the enclosure 10 is not shown for the convenience of presentation it being understood that it consists of a convection section, a roof and an outlet for allowing the combustion gases to discharge, also in a conventional manner.
  • a bed of particulate material shown in general by the reference numeral 18, is disposed within the enclosure 10 and rests on a perforated air distribution plate 20 which divides the enclosure 10 into an air plenum chamber 22 and a furnace section 24.
  • An air inlet 26 is provided through the lower portion of rear wall 14 in communication with the air plenum chamber 22 for distributing air from an external source (not shown) to the chamber.
  • Suitable air flow regulators can be mounted in the inlet 26 to vary the effective opening in the inlet 26 and thus control the flow of air into the chamber 22. Since the air flow regulators are of a conventional design and well known to those skilled in the art, they will not be described in an further detail.
  • the perforated air distribution plate 20 is adapted to support a bed 18 of particulate material consisting of inert material, a solid fuel material such as coal, and a sorbent material for the sulfur formed during combustion of the fuel if the fuel contains relatively large amounts of sulfur.
  • inert sand may be utilized in lieu of the sorbent.
  • the overall apparatus shown in Fig. 1 may, as an illustrative example, be incorporated into an appropriate heat transfer device wherein the heat produced by the bed which is fluidized during the combustion process is utilized to convert water to steam, such as in a steam generator.
  • the inner surfaces of the walls 12, 14 and 16 may be appropriately provided with suitable thermal insulation, such as refractory - material liners (not shown).
  • the perforated air distribution plate 20 includes a plurality of air distributors, or nozzles, 28 extending through a plurality of spaced openings formed through the plate 20.
  • the nozzles 28 are in the form of vertically disposed tubular members that extend upwardly from the plate 20 for a predetermined distance into the bed 18 of particulate material.
  • the nozzles 28 are spaced apart in the direction from front-to rear as shown in Fig. 1, it being understood that they are also spaced apart a predetermined distance from side-to-side so as to span the entire area enclosed by the walls 12, 14 and 16 and the sidewall that is not shown.
  • each nozzle 28 projects below the lower surface of the plate 20 and communicates with the air plenum chamber 22.
  • the upper end of each nozzle 28, as viewed in Fig. 1, may include a discharge arm 30 disposed at an acute angle to the vertically extending body portion 32 of the nozzle 28.
  • Fig. 2 shows a first embodiment of a nozzle 28 adapted for measurement of the static pressure therein for determining the rate of air flow into the bed 18 of particulate material according to the present invention.
  • the nozzle 28 includes an orifice plate 34 located at the inlet to the vertically extending body portion 32 of the nozzle 28. When air from the plenum 22 enters the nozzle 28, a flow profile is generated that varies with the downstream distance from the orifice plate 34.
  • a hole 36 is tapped into the body portion 32 of the nozzle 28 downstream of the orifice plate 34 and a pressure sensing device 38 is inserted into the hole 36.
  • a sensing line 40 is attached to the sensing device 38, and is directly routed to a differential pressure transmitter 42 or through an optional snubber-capacitor 44 as will be described.
  • the differential pressure transmitter 42 is attached to a sensing line 46 which senses the pressure in the air plenum 22 in a conventional manner.
  • the hole 36 preferably, is tapped at the location of the vena contracta which is the point at which the flow profile generated by the orifice plate 34 contracts to a minimum in accordance with conventional fluid flow principles.
  • the hole 36 is tapped downstream of the orifice plate 34 to avoid plugging of the pressure sensing device 38 caused by an accumulation of dust or very fine bed particles on the orifice plate 34 that enter the nozzle 28 by backflow when the reactor is shut down. Plugging of the pressure sensing device 38 can also be avoided by the addition of a filter (not shown) on the pressure sensing device 38 or by locating the device at a location further downstream from the orifice plate 34.
  • the static pressure is measured in a plurality of nozzles 28 to minimize sampling errors and to provide a statistically significant rate of air flow into and throughout the entire range of the bed 18 of particulate material. Nozzle-to nozzle flow differences are minimized by locating identical orifice plates 34 at the inlet of each nozzle 28.
  • a sensing line 40 from each of the plurality of nozzles 28 may be routed through the optional snubber-capacitor 44.
  • the snubber-capacitor 44 averages the pressure reading from the plurality of nozzles 28 and its volume is recommended to be at least three times the volume of all the sensing lines 40.
  • FIG. 3 illustrates a second embodiment of the present invention which includes components identical to some components of the previous embodiment which components are given the same reference numerals.
  • a venturi block 48 is located within the vertically extending body portion 32 of the nozzle 28.
  • the venturi block 48 preferably, is a solid piece of metal having a bell mouth inlet so that instead of generating a flow profile with a vena contracta, a consistent velocity is generated throughout the throat of the venturi block 48.
  • a hole 36 is tapped into the body portion 32 of the nozzle 28 at any point within the throat of the venturi block 48.
  • the pressure sensing device 38 is inserted into the hole 36 and, since there is a consistent velocity throughout the throat of the venturi block 48, the device 38 can obtain uniform and repeatable pressure measurements.
  • the sensing hole 36 is tapped downstream of the bell mouth but along the extension of the throat of the venturi block 48 so that there is no shelf upstream of the sensing hole 36 upon which particles can accumulate and block the pressure sensing device 38.
  • the venturi block 48 provides excellent mechanical strength for the sensing device 38.
  • the pressure sensing device 38 is connected to the sensing line 40 in a similar manner as described above in reference to Fig. 2.
  • the sensing line 40 may be directly routed to a differential pressure transmitter or, preferably, pressure is measured in a plurality of nozzles and a sensing line from each nozzle is routed to a snubber-capacitor, which communicates with a differential pressure transmitter.
  • Fig. 4 illustrates a third embodiment of the present invention in which the nozzle 28 does not include an orifice plate.
  • the hole 36 is tapped into the body portion 32 of the nozzle 28 at a point that is preferably at least five times the diameter of the nozzle body downstream of the nozzle inlet. In this manner, inconsistent flow measurements are minimized, since the turbulence created by entrance effects at the inlet of the nozzle have dissipated and uniform flow has developed thus yielding consistent readings from nozzle to nozzle.
  • the pressure sensing device 38 is inserted into the hole 36 and is connected in the same manner as described above in reference to Figs. 2 and 3.
  • the air flow regulators associated with the air inlet 26 are opened and air is distributed up through the air plenum chamber 22, toward the perforated air distribution plate 20 and into the inlet ends of the nozzles 28
  • the air then flows upwardly through the vertically extending body portions 32 of the nozzles 28 before it discharges from their discharge arm 30 into the bed 18 of particulate material.
  • the air discharges into the bed 18 in a direction generally toward the air distribution plate 20 to fluidize the particulate material and to prevent the formation of a dormant layer of particulate material between the surface of the air distribution plate 20 and the uppermost portion of the nozzles 28.
  • the bed particulate material provided on air distribution plate 20 is fired while air is introduced into the air plenum chamber 22.
  • Additional fuel and/or sorbent material is introduced by conventional means (not shown) and the fuel is ignited by burners (not shown) positioned within the bed. As the combustion of the fuel progresses, additional air is introduced into the air plenum chamber 22 in guantities sufficient to achieve substantially complete combustion.
  • the high-pressure, high velocity, combustion-supporting air introduced through the air distribution plate 20 from the air plenum chamber 22 is at a velocity which causes the bed 18 of particulate material to expand and take on a suspended or fluidized state.
  • the air is introduced at a velocity which is greater than the free fall velocity of the relatively fine particles in the bed and less than the free fall velocity of the relatively coarse particles.
  • the rate of air flow into the bed 18 is measured.
  • the rate of air flow into the bed 18 is measured by determining the differential pressure between the static pressure in the air plenum chamber 22 and the static pressure within at least one nozzle 28. Since the air flow within the nozzles 28 is at a high velocity, generally over 100 ft/sec, while the air flow within the plenum 22 is stagnant, or at a very low velocity, there will exist a substantial static pressure difference between these two locations.
  • the rate of air flow into the bed 18 of particulate material is determined from the difference in static pressure by means of conventional fluid mechanics calculations that are well-known to those skilled in the art.
  • pressure is measured, preferably, in a plurality of nozzles 28 to provide a statistically significant average pressure to represent the rate of air flow into and throughout the entire range of the bed 18 of particulate material.
  • the pressure is measured, preferably, at the same point in the flow profile generated in each nozzle 28 to ensure that uniform pressure measurements are obtained.
  • the pressure in the nozzle 28 is sent to the differential pressure transmitter 42 by means of the pressure sensing device 38 and the sensing line 40. Also, the pressure in the air plenum 22 is sent to the differential pressure transmitter 42 by means of the sensing line 46.
  • the differential pressure transmitter 42 determines the difference in pressure between the air plenum chamber 22 and the nozzle 28.
  • the pressure readings in a plurality of nozzles 28 are sent to the snubber capacitor 44 and are averaged in the snubber capacitor 44.
  • the snubber 44 dampens pressure oscillations, transients and fluctuations caused by unsteady air flow through the nozzles 28.
  • the average dampened pressure is sent to the differential pressure transmitter 42 which reads the difference in pressure between the air plenum chamber 22 and the snubber capacitor 44.
  • the fluidized bed reactor of the present invention in which the rate of air flow to the bed is measured provides several advantages. For example, by placing a sensing device within the body portion of a nozzle, the need for bulky ducting associated with a duct venturi and the need for an expensive hot wire anenometer or a honeycomb venturi grid are eliminated. Thus, substantial space and equipment cost savings are realized by the fluidized bed reactor of the present invention. Furthermore greater duct design flexibility is available by exclusion of duct venturis, and bed operation at stoichiometric conditions is realizable due to the improved airflow measurement accuracy.
  • the nozzles can be calibrated in a test bed which has a cold sand bed of typical bed height.
  • the dynamic offset to the differential pressure readings due to unsteady flow through the nozzles due to the chug/plug action of bed material above the nozzle can also be included in a nozzle calibration curve.
  • the fuel supplied to the furnace 24 can be in liquid or gaseous form rather than in the particulate solid form as described.
  • other variations can be made by those skilled in the art without departing from the invention as defined by the appended claims.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Measuring Volume Flow (AREA)
US07/304,998 1989-02-01 1989-02-01 Air flow measurement device for fluidized bed reactor Expired - Fee Related US4865540A (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
US07/304,998 US4865540A (en) 1989-02-01 1989-02-01 Air flow measurement device for fluidized bed reactor
CA000606485A CA1311157C (en) 1989-02-01 1989-07-21 Air flow measurement device for fluidized bed reactor
JP1200428A JPH0682055B2 (ja) 1989-02-01 1989-08-03 流動床反応器
CN89107388A CN1021478C (zh) 1989-02-01 1989-09-20 流化床反应器
EP19900300943 EP0381438A3 (de) 1989-02-01 1990-01-30 Wirbelbettreaktoren mit Luftstrommessgerät .
PT93042A PT93042A (pt) 1989-02-01 1990-02-01 Reactor de leito fluidificado e respectivo dispositivo de medicao de fluxo de ar

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US07/304,998 US4865540A (en) 1989-02-01 1989-02-01 Air flow measurement device for fluidized bed reactor

Publications (1)

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US4865540A true US4865540A (en) 1989-09-12

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Application Number Title Priority Date Filing Date
US07/304,998 Expired - Fee Related US4865540A (en) 1989-02-01 1989-02-01 Air flow measurement device for fluidized bed reactor

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US (1) US4865540A (de)
EP (1) EP0381438A3 (de)
JP (1) JPH0682055B2 (de)
CN (1) CN1021478C (de)
CA (1) CA1311157C (de)
PT (1) PT93042A (de)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5286188A (en) * 1992-09-11 1994-02-15 Foster Wheeler Energy Corporation Uni-directional anti-backsifting fluidization nozzle and a fluidized bed system utilizing same
WO2003033126A1 (en) * 2001-10-19 2003-04-24 Ariacon Oy Multifunction fluid bed apparatus and method for processing of material in a fluid bed apparatus
US20040172765A1 (en) * 2003-03-04 2004-09-09 Rodney England Mattress
WO2008066843A1 (en) * 2006-11-30 2008-06-05 Westlake Longview Corporation Gas distribution plate for fluidized-bed olefin polymerization reactors equipped with flowrate or pressure sensors to detect grid fouling
CN100435928C (zh) * 2006-09-20 2008-11-26 浙江大学 一种气体分布器
US20080318172A1 (en) * 2004-06-23 2008-12-25 Ebm-Papst Landshut Gmbh Method for Regulating and Controlling a Firing Device and a Firing Device
US20100018444A1 (en) * 2008-07-25 2010-01-28 Alstom Technology Ltd Fuel fluidizing nozzle assembly
WO2010011457A3 (en) * 2008-07-25 2010-03-18 Alstom Technology Ltd Fuel fluidizing nozzle assembly
WO2018113417A1 (zh) * 2016-12-23 2018-06-28 中国石油化工股份有限公司 流化床反应器的进料分布器的压降控制系统和控制方法
US10195582B2 (en) * 2010-11-08 2019-02-05 Ze Energy Inc. Gasification furnace, gasification system, reformer and reforming system
KR20210113730A (ko) * 2020-03-09 2021-09-17 주식회사 멘도타 고품위 활성탄의 제조 장치 및 그 제조 방법
US11598519B2 (en) 2017-04-28 2023-03-07 Sumitomo SHI FW Energia Oy Fluidizing gas nozzle head and a fluidized bed reactor with multiple fluidizing gas nozzle heads

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FR2723003B1 (fr) * 1994-07-28 1996-09-13 Gec Alsthom Stein Ind Procede et dispositif de controle de la circulation interne dans un reacteur a lit fluidise et reacteur equipe d'un tel dispositif
JP3220375B2 (ja) * 1996-04-16 2001-10-22 東洋エンジニアリング株式会社 詰まり検知方法および造粒方法
CN102042587B (zh) * 2009-10-14 2012-09-19 财团法人工业技术研究院 流体化床燃烧炉及其控制方法
CN105526581A (zh) * 2015-12-29 2016-04-27 广西节得乐生物质能源科技有限公司 一种生物质气化燃烧器

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Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5286188A (en) * 1992-09-11 1994-02-15 Foster Wheeler Energy Corporation Uni-directional anti-backsifting fluidization nozzle and a fluidized bed system utilizing same
WO2003033126A1 (en) * 2001-10-19 2003-04-24 Ariacon Oy Multifunction fluid bed apparatus and method for processing of material in a fluid bed apparatus
US20040172765A1 (en) * 2003-03-04 2004-09-09 Rodney England Mattress
US20110033808A1 (en) * 2004-06-23 2011-02-10 Ebm-Papst Landshut Gmbh Method for regulating and controlling a firing device and firing device
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EP0381438A3 (de) 1990-12-05
CA1311157C (en) 1992-12-08
PT93042A (pt) 1991-10-15
EP0381438A2 (de) 1990-08-08
CN1021478C (zh) 1993-06-30
JPH02228523A (ja) 1990-09-11
CN1044704A (zh) 1990-08-15
JPH0682055B2 (ja) 1994-10-19

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